Patent Application
20060042525
The present application relates generally to fossil fuel boilers and, more particularly, to optimizing Selective Catalytic Reduction (SCR) performance in fossil fuel boilers.
The combustion of coal and other fossil fuels during the production of steam or power produces dozens of gaseous oxides, such as NO, NO2, N2O, H2O, HO, O2H, CO, CO2, SO, SO2, etc. which together, with N2 and excess O2, make up the overwhelming majority of the boiler flue gas. Many of these species, such as OH and O2H are highly reactive and are chemically quenched prior to the flue gas exit from the boiler stack. Some of the species, such as CO, CO2, and H2O are highly stable, the vast majority of which will pass unreacted out of the boiler stack. Still other species, such as SO2, NO, and NO2 are moderately reactive. These moderately reactive species are subject to removal from the flue gas by chemical reaction processes, and are also subject to complex variability.
NO and NO2, together referred to as NOx, are gases that are highly toxic to humans. NOx can combine with H2O to form nitric acid in the lungs and other mucosal membranes. In addition, NOx can react with O2 in the lower troposphere to form ozone, also a toxic gas. For these and other reasons, including federal and state legislation, many industrial power plants need to find ways to cost effectively reduce the flue gas NOx to acceptable emission levels.
NOx levels out of the furnace of industrial coal burning power plants vary, depending upon the particular combustion technology, typically from about 100 parts per million (ppm) to greater than one thousand ppm. NOx levels out of the furnace of industrial oil and gas burning power plants vary less, because of the consistency of the fuel sources, from about 100 ppm to 600 ppm. Oil and gas combustion tend to produce lower levels of NOx than does coal combustion because there is little nitrogen found within oil or gas, and because they tend to burn at lower temperature than coal due to their relatively simple molecular structures. Desirable emission levels vary, depending upon many factors including plant location, stack height, furnace NOx levels, and state laws and provisions. Desirable emission levels may be expressed as an absolute number, e.g. less than 50 ppm, or as a percentage reduction from the furnace NOx levels. Desirable NOx emission levels can be as low as 10 ppm.
A number of technologies have been adapted by industrial power plants in order to reduce furnace NOx levels to acceptable emission levels. These include SCR, Selective NonCatalytic Reduction (SNCR), boiler optimization and tuning, the use of Over Fire Air (OFA) and other vertical staging of furnace air introduction techniques, and the use of low NOx burners. Each method has a typical NOx reduction range that tends to correlate well with the cost the market will bear for the device. Of the methods listed, the SCR is capable of removing the greatest quantities of NOx from the flue gas but does so at a very high cost. Design and installation costs for industrial SCRs run into hundreds of millions of U.S. dollars. Annual operational costs, including reducing reagent, maintenance, and catalyst replacement, for an industrial SCR can run into the millions of dollars.
An SCR works by adding a reactive chemical reducing agent into the flue gas in appropriate stoichiometric amounts so that it may react with the NOx molecules and undergo a chemical reaction into harmless byproducts. A catalyst, typically a solid phase metal oxide deposited on a support structure, is used to accelerate the rate of key steps in the chemical reactions. Typically, a catalyst will drop the energy of activation for a reaction by transiently binding with one or more of the reagents. One of the most commonly used catalysts found in SCR is di-Vanadium Pentoxide (V2O5). In addition to the active catalytic molecule, SCRs may contain molecules whose purpose is to impact other important reactions, such as impeding the catalyst poisoning from Na, K, AsO3, Pb, P, Cl, F, etc. The additives vary between vendors and differ according to the SCR design, fuel being burned, and other factors.
Nearly all SCRs use ammonia (NH3) as the reducing reagent. Though there are many reactions that may be used to reduce NOx into harmless byproducts, one of the more common is
NH3+NO+¼O2→1½H2O+N2
indicating that ammonia and NO combine in a one to one ratio, and with oxygen in a 4 to 1 ratio, to produce water and nitrogen gas. This and other reaction mechanisms indicate the actual stoichiometric ratio of NOx and reducing reagent that get consumed by the reaction. If the actual flue gas contains an excess of either ammonia or NOx, that excess will leave the SCR, where it can subsequently react or remain in the flue gas until it exits at the stack. Excess ammonia is considered undesirable because it can render trapped fly-ash unsellable due to odor and because it is a very toxic and corrosive gas that should not exit the stack in even small amounts. Excess NOx is considered undesirable because this indicates that the SCR was not operating at its full potential efficiency. Excess NOx or ammonia are referred to as “slip”.
SCR manufacturers have developed numerous methods and devices in an attempt to achieve the tightest stoichiometric matching of injected reducing reagent to furnace NOx, and thereby achieving the highest effectiveness and efficiency of SCR performance. There are several challenges to matching the stoichiometry of the reagent and the NOx.
One challenge to SCR optimization is to adjust the ammonia injection to the continuously varying distribution of NOx that comes out of the furnace. Levels of NOx can vary by a factor of two or more as measured laterally, front to back or left to right, across the duct. The variations can happen rapidly and are a function of both exogenous (outside of the immediate operator or automatic control) and endogenous factors. Factors include load, temperature, coal type, unit load, burner tilts, lateral fuel biases, lateral air biases, LOI, turbulence, coal particle size, vertical fuel bias, and vertical air bias, including OFA.
Rather than grapple with the problem of constantly matching the reagent injection profile to the NOx profile at all points along the two dimensions of lateral traversal across the duct, some SCR designs rely on the use of mixers to generally remove all lateral variations in the boiler NOx profile. Ammonia may then be injected into the mixed flue gas and the combined gases then mixed again, to attempt to ensure the equal distribution of the ammonia. This method has a thermodynamic efficiency cost related to the loss of exergy from the mixing process. The greater the mixing, the greater the thermodynamic efficiency cost. The effectiveness and corresponding design of mixing devices is dependent in part on the flue gas velocity. Since the mixing devices typically are static structures, they are, by design, only optimized for mixing at the design load. As a result, the mixing efficiency will be sub-optimal at various, off-design, times of operation. Areas with less than perfect mixing will result in poor stoichiometry and associated slip of either NOx or ammonia.
Another way to manage the variability of the NOx distribution is to enable the automated and real time manipulation of the reagent injection profile so that it can be adjusted to match the NOx distribution. A drawback to this method is that it requires the manipulation of multiple valves in the ammonia injection grid (AIG). There is an installation expense to configuring multiple valves for actuation, an operational expense to enabling the real time manipulation of multiple AIG valves, and a complication and associated hazard of adding any movable part into an ammonia system. At present, very few SCRs in the U.S. are designed with this degree of on line control built into the AIG.
Another way to manage the variability of the NOx distribution is to enable the manipulation of the reagent injection profile on a non-real time, periodic basis. Most SCRs in the U.S. use this method, first tuning the AIG profile at commissioning of the SCR and then again on an annual basis. The tuning procedure includes identification of the typical NOx distribution patterns from the boiler and subsequent adjustment of the AIG valves to achieve the desired stoichiometry. The AIG valves are then fixed in this position until the next study is performed. There are numerous drawbacks to this methodology. First, the tuning is optimized for the typical, modal (design) load factors of the boiler. At off-design loads the NOx distribution will change and will result in additional NOx slip or ammonia slip. Another drawback to this method is that it cannot compensate for the slow drifts that occur in the NOx distribution at the modal (and other) load over the period of a year. Another drawback to this method is that it cannot compensate for the variations that occur in furnace NOx distribution that result from different operator or automatic controllers that manipulate burner tilts, lateral fuel biases, lateral air biases, LOI, turbulence, coal particle size, vertical fuel bias, and vertical air bias, including OFA. In effect, this method is optimized for operation at the modal NOx distribution of the furnace and is sub-optimal at all other conditions, resulting in additional NOx slip or ammonia slip.
The lateral furnace NOx profile can change as a function of air and fuel introduction parameters because NOx is created largely out of the Oxygen found in the air and Nitrogen found in the fuel. However, NOx profiles and, more importantly, integrated NOx quantities are strongly dependent upon the combustion temperature of the furnace and therefore upon the load of the unit. The very strong temperature dependence of NOx formation is a result of the usually exponential dependence of chemical reaction rates on temperature.
As a result, another challenge to SCR optimization is to adjust the net ammonia injection amount into the flue gas as a function of combustion temperature. Because combustion temperature is expensive to measure continuously and reliably, most SCRs do not use it as the input parameter for injected ammonia, but rather use unit load, a good proxy for combustion temperature, as the input parameter. Typically, design curves are used to represent the total furnace NOx production as a function of unit load. The load based NOx design curves are typically created during the commissioning of the SCR and may be updated periodically over the life of the SCR. The load based NOx curves are typically used by the DCS or other automated control system for the feed forward control of the total amount of injected ammonia. In particular, as unit load goes up, the feed forward control will anticipate the increased production of furnace NOx and will adjust the total ammonia injection levels accordingly. One drawback to feed forward control is that it does not make adjustments to the injected ammonia as a function of any variable except that which is specified in the curve. So, for instance, a large change in furnace NOx production resulting from a change in coal type would not result in a change in total ammonia injection. For this reason, most SCR control systems that deploy a feed forward control loop also deploy a feed back control loop.
The feedback control loop of the SCR is typically designed to measure the NOx slip (NOx level in the stack) and adjust the feed forward specified ammonia injection amount so as to maintain a constant NOx slip or percentage NOx removal. The feedback loop can therefore correct for variations of total furnace NOx productions that differ from the load based design curves.
Another challenge to SCR optimization is to make accommodations for the fact that the catalyst will degrade and will degrade non-isotropically. Non-isotropic degradation of the catalyst leads to certain flow lines through the catalyst bed having greater or lesser integrated activity than the average. As the average integrated activity drops, those flow lines of lesser activity than average can eventually reach a critical level where complete reaction of the NOx and the ammonia no longer occurs, resulting in both NOx and ammonia slip along those flow lines. This situation is particularly difficult to manage because the standard SCR feedback loops will see an increase in NOx slip and will correct for it by increasing the injected ammonia, which will have the unintended affect of increasing ammonia slip.
The catalyst degradation itself can be due to a number of factors. These factors include high flue gas temperatures (which lead to a phase transition of the catalyst); plugging of the catalyst pores and masking of the catalyst surface (with Calcium and Ammonium sulfate salts or with fly ash); and poisoning of the active catalytic sites (with Na, K, AsO3, Pb, P, Cl, F, etc.).
Non-isotropic catalyst degradation can result from a number of sources. One source is the maldistribution of furnace gases resulting from poorly balanced combustion conditions. Since the flue gas in most industrial power plants is subject to laminar flow conditions, maldistributions at the furnace can manifest in the SCR. Another related source of non-isotropic degradation are temperature spikes along certain flow lines resulting from non-isotropic cleaning of the heat transfer surfaces in the back pass. Another source of non-isotropic degradation is from high levels of ammonia injections in parts of the AIG that lead to enhanced ammonium sulfate condensation in the SCR. Yet another source of non-isotropic degradation is from systematic errors in sootblowing of the catalyst bed.
The overall activity level of the catalyst bed can be defined as a number between 1 and 0, where 1 indicates a completely active, usually fresh and clean, surface and where 0 indicates no active surface remaining. Recommendations vary according to manufacturer, but catalyst beds are typically changed out when the activity drops to anywhere between 0.5 and 0.9. Since changing the catalyst is a very expensive proposition, extending the usable life of the catalyst is desirable. Regardless of the activity level of the catalyst, catalyst change or addition is usually required when ammonia slip levels exceed a certain design specification, which is usually in the range of 2-5 ppm.
Industrial SCRs are built with an excess of catalyst. If the challenges to SCR control described above could be resolved, these SCRs could operate at 100% NOx removal efficiency with negligible ammonia slip. Instead, most SCRs operate at about 80-90% removal efficiency. Enhanced control of these challenges is therefore desirable.
In accordance with one or more embodiments of the invention, a system is provided for controlling SCR performance in a boiler. The boiler includes one or more generally cross sectional areas. Each cross sectional area can be characterized by one or more profiles of one or more conditions affecting SCR performance and be associated with one or more adjustable desired profiles of the one or more conditions during the operation of the boiler. The performance of the boiler can be characterized by boiler performance parameters. A system in accordance with one or more embodiments of the invention can include a controller input for receiving a performance goal for the boiler corresponding to at least one of the boiler performance parameters and for receiving data values corresponding to boiler control variables and to the boiler performance parameters. The boiler control variables include one or more current profiles of the one or more conditions. The system also includes a system model that relates one or more profiles of the one or more conditions in the boiler to the boiler performance parameters. The system also includes an indirect controller that determines one or more desired profiles of the one or more conditions to satisfy the performance goal for the boiler. The indirect controller uses the system model, the received data values and the received performance goal to determine the one or more desired profiles of the one or more conditions. The system model also includes a controller output that outputs the one or more desired profiles of the one or more conditions.
In accordance with one or more embodiments of the invention, a system is provided for determining one or more desired operating settings for one or more devices affecting SCR performance in a fossil fuel boiler. The operation of the one or more devices can be characterized by adjustable operating settings. The performance of the boiler can be characterized by boiler performance parameters. The system includes a controller input for receiving a performance goal for the boiler corresponding to at least one of the boiler performance parameters and for receiving data values corresponding to boiler control variables and to the boiler performance parameters. The system also includes a system model that relates operating settings for the one or more devices to the boiler performance parameters. The system also includes an indirect controller that determines one or more desired operating settings for the one or more devices to satisfy the received performance goal for the boiler using the system model, and using the received performance goal for the boiler and the received data values. The system also includes a controller output that outputs the one or more desired operating settings for the one or more devices.
In accordance with one or more embodiments of the invention, a system is provided for determining one or more desired profiles of one or more conditions affecting SCR performance in a boiler. The boiler has one or more generally cross sectional areas, each being characterized by one or more profiles of the one or more conditions and being associated with one or more adjustable desired profiles of the one or more conditions during the operation of the boiler. The performance of the boiler can be characterized by boiler performance parameters. The system includes a controller input for receiving a performance goal for the boiler corresponding to at least one of the boiler performance parameters and for receiving data values corresponding to boiler control variables and to the boiler performance parameters. The boiler control variables include one or more current profiles of the one or more conditions. The system also includes a direct controller that determines one or more desired profiles of the one or more conditions to satisfy the performance goal for the boiler. The direct controller uses the received data values and the received performance goal to determine the one or more desired profiles of the one or more conditions. The system also includes a controller output that outputs the one or more desired profiles of the one or more conditions.
In accordance with one or more embodiments of the invention, a system is provided for determining one or more desired operating settings for one or more devices affecting SCR performance in a fossil fuel boiler. The operation of the one or more devices can be characterized by adjustable operating settings. The performance of the boiler can be characterized by boiler performance parameters. The system includes a controller input for receiving a performance goal for the boiler corresponding to at least one of the boiler performance parameters and for receiving data values corresponding to boiler control variables and to the boiler performance parameters. The system also includes a direct controller that determines one or more desired operating settings for the one or more devices to satisfy the received performance goal for the boiler using the received performance goal for the boiler and the received data values. The system also includes a controller output that outputs the one or more desired operating settings for the one or more devices.
In accordance with one or more embodiments of the invention, a system is provided for controlling SCR performance in a fossil fuel boiler. The boiler includes one or more generally cross-sectional areas, each cross-sectional area defining a profile of a condition at the cross-sectional area. The system includes one or more devices associated with the one or more cross-sectional areas for adjusting the profile at a cross-sectional area. The one or more devices operate in accordance with adjustable operating parameters. The system also includes one or more sensors associated with the one or more cross-sectional areas for detecting conditions at the one or more cross-sectional areas. The system also includes an indirect controller that determines operating settings for the one or more devices. The indirect controller includes a system model that relates operating settings for the one or more devices to desired profiles of the conditions. The indirect controller has a controller input in communication with the one or more sensors. The indirect controller uses the conditions detected by the one or more sensors, the system model, and the desired profiles to determine operating settings for the one or more devices. The indirect controller further includes a controller output in communication with the one or more devices to transmit the operating settings to the one or more devices.
In accordance with one or more embodiments of the invention, a method is provided for determining one or more desired profiles of one or more conditions in a boiler. The boiler has one or more generally cross-sectional areas, each cross-sectional area being characterized by a profile of a condition and being associated with a desired profile of the condition during the operation of the boiler. The performance of the boiler can be characterized by one or more boiler performance parameters. The method includes the steps of: (a) implementing a controller with a system model that relates the one or more profiles in the boiler to the performance of the boiler; (b) obtaining a performance goal for the boiler; (c) receiving data corresponding to the boiler performance parameters and boiler control variables; (d) determining an operating point corresponding to the performance goal using the system model; (e) determining one or more desired profiles associated with the operating point using the system model; and (f) communicating the one or more desired profiles to one or more subsystems operable to adjust one or more profiles.
In accordance with one or more embodiments of the invention, a method is provided for determining desired operating settings for one or more devices affecting SCR performance in a boiler. The operation of the one or more devices can be characterized by one or more operating parameters. The performance of the boiler can be characterized by one or more boiler performance parameters. The method can include the steps of: (a) implementing a controller with a system model that relates the operating parameters of the one or more to the boiler performance parameters; (b) obtaining a performance goal for the boiler; (c) receiving data corresponding to the boiler performance parameters and boiler control variables; (d) determining an operating point corresponding to the performance goal using the system model; (e) determining operating settings of the one or more devices associated with the operating point using the system model; (f) determining a control move using the operating settings determined in step (e) for directing the boiler to the operating point; and (g) communicating the control move to the one or more devices to adjust operating parameters of the one or more devices.
In accordance with one or more embodiments of the invention, a method is provided for controlling one or more profiles of conditions in a boiler. The boiler has one or more generally cross-sectional areas, each having a profile of a condition and is associated with a desired profile during the operation of the boiler. The performance of the boiler can be characterized by boiler performance parameters. The method can include the steps of: (a) providing a direct controller that determines one or more desired profiles in relation to a boiler performance goal; (b) obtaining a performance goal for the boiler; (c) determining whether the performance goal is satisfied by current boiler performance; (d) when the performance goal is not satisfied, identifying the generally closest operating region in which the performance goal would be satisfied, the operating region being associated with one or more desired profiles; and (e) outputting the one or more desired profiles.
In accordance with one or more embodiments of the invention, a method is provided for adjusting operating settings of one or more devices affecting SCR performance in a boiler. The boiler has one or more generally cross-sectional areas. Each of the one or more devices is associated with a cross-sectional area. Each cross-sectional area has a profile of a condition and is associated with a desired profile. The performance of the boiler is characterized by boiler performance parameters. The method can include the steps of: (a) providing a direct controller that determines desired operating settings of the one or more devices in relation to a performance goal for the boiler; (b) obtaining a performance goal for the boiler; (c) determining whether the performance goal is satisfied by current boiler performance; (d) when the performance goal is not satisfied, identifying the generally closest operating region in which the performance goal would be satisfied using the direct controller, the operating region being associated with desired operating parameters of the one or more devices; (e) determining a control move using the desired operating parameters of the one or more devices for directing the boiler to the operating region; and (f) communicating the control move to the one or more devices.
In accordance with one or more embodiments of the invention, a method is provided for adjusting operating settings for one or more devices affecting one or more profiles of conditions affecting SCR performance in a boiler. The boiler includes one or more generally cross-sectional areas. Each of the one or more devices is associated with a cross-sectional area. Each cross-sectional area has a profile of a condition. The method can include the steps of: (a) providing an indirect controller with a system model that relates the operating settings of the one or more devices to respective profiles; (b) providing data values to the indirect controller indicative of actual profiles; (c) providing one or more desired profiles to the indirect controller; (d) determining desired operating settings for the one or more devices, to attain the desired respective profiles using the indirect controller; (e) determining a control move derived from the desired operating settings; and (f) communicating the control move to the one or more devices.
These and other features and advantages of the present invention will become readily apparent from the following detailed description, wherein embodiments of the invention are shown and described by way of illustration of the best mode of the invention. As will be realized, the invention is capable of other and different embodiments and its several details may be capable of modifications in various respects, all without departing from the invention. Accordingly, the drawings and description are to be regarded as illustrative in nature and not in a restrictive or limiting sense, with the scope of the application being indicated in the claims.
In the drawings, like reference numbers are used to generally denote like parts.
The terms “optimal,” “optimize,” and “optimization” and the like as used herein refer to generally to improving (e.g., efficiency, effectiveness or performance) and are not intended to require attaining ideal performance or any particular best value.
As illustrated in
The boiler 100 includes a NOx and NH3 slip removal optimization system 126, which can include a controller 128 that configures one or more (preferably all) of the fuel/air injection, ammonia injection, and catalyst soot blow control interfaces 130 in communication with fuel/air injectors 104, ammonia injection grid 118, and catalyst sootblowers 120, respectively. The control interfaces 130 can include a Distributed Control System, DCS, with additional control logic directed towards the fuel/air injectors 104, ammonia injection grid 118, and catalyst sootblowers 120. The NOx and NH3 slip removal optimization system 126 can adjust one or more (preferably all) of the fuel/air injection, NH3 injection, and catalyst sootblowing operating parameters according to desired boiler performance goals using the controller 128. In the illustrated embodiment, controller 128 is a direct controller (i.e., one that does not use a system model). As discussed below, in various embodiments, NOx and NH3 slip removal optimization system 126 may include either a direct controller or an indirect controller (i.e., one that uses a system model). In embodiments in which the optimization system 126 incorporates a direct controller such as controller 128, it can execute and optionally adapt (if it is adaptive) a control law that drives boiler 100 toward the boiler performance goals. Direct control schemes in various embodiments of the invention can include, e.g., a table or database lookup of control variable settings as a function of the process state, and also include a variety of other systems, involving multiple algorithms, architectures, and adaptation methodologies. In one or more embodiments, the direct controller is implemented in a single phase.
In one or more embodiments, controller 128 can be a steady state or dynamic controller. A physical plant, such as boiler 100, is a dynamic system, namely, it is composed of materials that have response times due to applied mechanical, chemical, and other forces. Changes made to control variables or to the state of boiler 100 are, therefore, usually accompanied by oscillations or other movements that reflect the fast time-dependent nature and coupling of the variables. During steady state operation or control, the boiler 100 reaches an equilibrium state such that a certain set or sets of control variable settings enable maintenance of a fixed and stable plant output of a variable such as megawatt power production. Typically, however, boiler 100 operates and is controlled in a dynamic mode. During dynamic operation or control, the boiler 100 is driven to achieve an output that differs from its current value. In certain embodiments, the controller 128 is a dynamic controller. In general, dynamic controllers include information about the trajectory nature of the plant states and variables. In some embodiments, controller 128 can also be a steady-state controller used to control a dynamic operation, in which case the dynamic aspects of the plant are ignored in the control and there is a certain lag time expected for the plant to settle to steady state after the initial process control movements.
In accordance with one or more embodiments of the invention, three general classes of modeling methods can be used for the construction of direct controller 128. One method is a strictly deductive, or predefined, method. A strictly deductive method uses a deductive architecture and a deductive parameter set. Examples of deductive architectures that use deductive parameter sets include parametric models with preset parameters such as first principle or other system of equations. Other strictly deductive methods can include preset control logic such as if-then-else statements, decision trees, or lookup tables whose logic, structure, and values do not change over time.
Controller 128 is preferably adaptive, to capture the off-design or time-varying nature of boiler 100. A parametric adaptive modeling method can also be used in various embodiments of the invention. In parametric adaptive modeling methods, the architecture of the model or controller is deductive and the parameters are adaptive, i.e., are capable of changing over time in order to suit the particular needs of the control system. Examples of parametric adaptive modeling methods that can be used in some embodiments of the invention include regressions and neural networks. Neural networks are contemplated to be particularly advantageous for use in complex nonlinear plants, such as boiler 100. Many varieties of neural networks, incorporating a variety of methods of adaptation, can be used in embodiments of the present invention.
Another type of modeling method, strictly non-parametric, that can also be used in one or more embodiments of the invention uses an adaptive architecture and adaptive parameters. A strictly non-parametric method has no predefined architecture or sets of parameters or parameter values. One form of strictly non-parametric modeling suitable for use in one or more embodiments of the invention is evolutionary (or genetic) programming. Evolutionary programming involves the use of genetic algorithms to adapt both the model architecture and its parameters. Evolutionary programming uses random, but successful, combinations of any set of mathematical or logical operations to describe the control laws of a process.
In embodiments in which controller 128 is adaptive, it is preferably implemented on-line, or in a fully automated fashion that does not require human intervention. The particular adaptation methods that are applied are, in part, dependent upon the architecture and types of parameters of the controller 128. The adaptation methods used in one or more embodiments of the invention can incorporate a variety of types of cost functions, including supervised cost functions, unsupervised cost function and reinforcement based cost functions. Supervised cost functions include explicit boiler output data in the cost function, resulting in a model that maps any set of boiler input and control variables to the corresponding boiler output. Unsupervised cost functions require that no plant output data be used within the cost function. Unsupervised adaptation is primarily for cluster or distribution analysis.
In one or more embodiments of the invention, a direct controller may be constructed and subsequently adapted using a reinforcement generator, which executes the logic from which the controller is constructed. Reinforcement adaptation does not utilize the same set of performance target variable data of supervised cost functions, but uses a highly restricted set of target variable data, such as ranges of what is desirable or what is bad for the performance of the boiler 100. Reinforcement adaptation involves training the controller on acceptable and unacceptable boiler operating conditions and boiler outputs. Reinforcement adaptation therefore enables controller 128 to map specific plant input data to satisfaction of specific goals for the operation of the boiler 100.
One or more embodiments of the invention can use a variety of search rules that decide which of a large number of possible permutations should be calculated and compared to see if they result in an improved cost function output during training or adaptation of the model. In one or more embodiments, the search rule used may be a zero-order, first-order or second-order rule, including combinations thereof. It is preferred that the search rule be computationally efficient for the type of model being used and result in global optimization of the cost function, as opposed to mere local optimization. A zero-order search algorithm does not use derivative information and may be preferred when the search space is relatively small. One example of a zero-order search algorithm useful in embodiments of the invention is a genetic algorithm that applies genetic operators such as mutation and crossover to evolve best solutions from a population of available solutions. After each generation of genetic operator, the cost function may be reevaluated and the system investigated to determine whether optimization criteria have been met. While the genetic algorithms may be used as search rules to adapt any type of model parameters, they are typically used in evolutionary programming for non-parametric modeling.
A first-order search uses first-order model derivative information to move model parameter values in a concerted fashion towards the extrema by simply moving along the gradient or steepest portion of the cost function surface. First-order search algorithms are prone to rapid convergence towards local extrema, and it is generally preferable to combine a first-order algorithm with other search methods to provide a measure of global certainty. In some embodiments of the invention, first-order searching is used in neural network implementation. A second-order search algorithm utilizes zero, first, and second-order derivative information.
In one or more embodiments of the invention, controller 128 is generated in accordance with the control variables available for manipulation and the types of boiler performance objectives defined for boiler 100. Control variables can be directly manipulated in order to achieve the control objectives, e.g., reduce NOx output. As discussed above, in certain embodiments, the SCR operating parameters are control variables that controller 128 manages directly in accordance with the overall boiler objectives. Significant performance parameters may include, e.g., emissions (NOx), heat rate, opacity, and capacity. The heat rate or NOx output may be the primary performance factor that the SCR optimization system 126 is designed to regulate. Desired objectives for the performance parameters may be entered into the controller 128, such as by an operator, or may be built into the controller 128. The desired objectives may include specific values, e.g., for emissions, or more general objectives, e.g., generally minimizing a particular performance parameter or maintaining a particular range for a parameter. Selecting values or general objectives for performance parameters may be significantly easier initially than determining the corresponding SCR operating settings for attaining those performance values. Desired values or objectives for performance parameters are generally known beforehand, and may be dictated by external requirements. For example, for the heat rate, a specific maximum acceptable level may be provided to controller 128, or controller 128 may be instructed to minimize the heat rate.
In one or more embodiments, controller 128 is formed of a neural network, using a reinforcement generator to initially learn and subsequently adapt to the changing relationships between the control variables, in particular, the SCR operating parameters, and the acceptable and unacceptable overall objectives for the boiler. The rules incorporated in the reinforcement generator may be defined by a human expert, for example. The reinforcement generator identifies the boiler conditions as favorable or unfavorable according to pre-specified rules, which include data values such as NOx emission thresholds, stack opacity thresholds, CO emission thresholds, current plant load, etc. For example, the reinforcement generator identifies a set of sootblowing operating parameters as part of a vector that contains the favorable-unfavorable plant objective data, for a single point in time. This vector is provided by the reinforcement generator to controller 128 to be used as training data for the neural network. The training teaches the neural network to identify the relationship between any combination of SCR operating parameters and corresponding favorable or unfavorable boiler conditions. In a preferred embodiment, controller 128 further includes an algorithm to identify the preferred values of SCR operating parameters, given the current values of SCR operating parameters, as well as a corresponding control sequence. In certain contemplated embodiments, the algorithm involves identifying the closest favorable boiler operating region to the current region and determining the specific adjustments to the SCR operating parameters that are required to move boiler 128 to that operating region. Multiple step-wise SCR operating parameter adjustments may be required to attain the closest favorable boiler objective region due to rules regarding SCR operating parameter allowable step-size or other constraints.
In accordance with one or more embodiments, an exemplary method for controlling SCRs 104 and boiler fuel and air injection systems using controller 128 is shown in
Radius2=ΣiNαi(S.P2i-proposed−S.P2i-current)2
for each ith SCR parameter, up to SCR parameter number N, with normalization coefficients αi. The sweep looks to identify a point on the boiler objective surface with a favorable value. If one is found in the first sweep, the radius is reduced, and the sweep repeated until the shortest distance (smallest radius) point has been identified. If a favorable plant objective surface point is not found upon the first sweep of radius r, then the radius is increased, and the sweep repeated until the shortest distance (radius) point has been identified. In a one or more embodiments, multiple SCR and boiler parameters may need to be adjusted simultaneously at the closest favorable control region. By way of example, the SCR parameter values can include unit load and furnace temperature, vertical and horizontal fuel and air distribution settings that directly impact total furnace NOx and furnace NOx distributions; total NH3 injection settings; NH3 left/right and front/back bias settings; SCR inlet gas temperature; catalyst cleanliness and catalyst activity distributions, etc. In addition to identifying the closest control variable region that allows for satisfying the performance goal, controller 128 also determines a sequence of control moves in step 208. A number of control moves may be required because controller 128 may be subject to constraints on how many parameters can be changed at once, how quickly they can be changed, and how they can be changed in coordination with other parameters that are also adjusted simultaneously, for example. Other constraints may exist that limit the objective value of the performance goal, rather than limiting the rate at which controls may be moved to achieve the desired objective. For instance, if the performance goal is to minimize stack NOx, a constraint to limit the NH3 slip should be built. This constraint would limit the amount and distribution of NH3 injection and or NOx distribution so that the lowest stack NOx objective would be targeted that would be consistent with the specified NH3 slip constraint. Controller 128 determines an initial control move. In step 210, it communicates that control move to the SCR and boiler manipulatable controls, for example, through control interface 130. In step 212, fuel/air injection 104, ammonia injection 118, and catalyst sootblowers 120 operate in accordance with the desired operating settings. After a suitable interval, indicated in step 214, preferably when the response to the fuel/air injection, ammonia injection, and catalyst sootblowing operations are stable, the operating parameters and boiler outputs, i.e., indicators of actual boiler performance, are stored in step 216. Additionally, satisfaction of the performance goal is also measured and stored. In particular, the system may store information about whether the NOx level is satisfactory or has shown improvement. The control sequence is then repeated. In some embodiments, the identified SCR and boiler operating settings may not be reached because the performance goal or boiler operating conditions may change before the sequence of control moves selected by the controller for the previous performance goal can be implemented, initiating a new sequence of control moves for the SCR and boiler operation.
As shown in
As illustrated in
In accordance with one or more embodiments, the system model 316 can represent a committee of models. In one or more embodiments of the invention incorporating an indirect controller, controller 310 may use any number of model architectures and adaptation methods. Various implementation techniques previously described in conjunction with controller 128 are also applicable to model 316. In general, model 316 predicts the performance of the boiler under different combinations of the control variables.
In one or more embodiments, system model 316 is a neural network, mass-energy balance model, genetic programming model, or other system model. Models can be developed using data about the actual performance of the boiler 300. For example, a neural network or genetic programming model can be trained using historical data about the operation of the boiler. A mass-energy balance model can be computed by applying first principles to historical or real-time data to generate equations that relate the performance of boiler 300 to the state of boiler 300 and the SCR sootblower, fuel and air, and NH3 injection operating parameters. Data that is collected during subsequent operation of the boiler 300 can later be used to re-tune system model 316 when desired.
After a suitable interval, preferably after the plant response is determined to be stable at 414, the SCR sootblower, fuel and air, and NH3 injection operating parameters and plant outputs, such as the NOx output, are stored at 416. The control cycle is repeated after suitable intervals.
As shown in
In one or more alternate embodiments, shown, e.g., in
As illustrated, a single controller 128, 310, or 510 or processor 512 can handle control of all of the cross sectional slices 116 in the boiler. Alternatively, multiple controllers or processors may be provided to handle the cross sectional slices 116 in the boiler.
In another embodiment of the invention, processor 512 is an indirect controller that incorporates a system model that relates the catalyst sootblower, NH3 injector, and fuel and air injector operating parameters to the catalyst activity, NOx, and NH3 profiles in cross sectional slices 116. Processor 512 can use a process similar to the process shown in
In one or more embodiments of the invention a single controller, as, e.g., described previously as controller 510, may be integrated with processor 512 and control interface 514. In this integrated embodiment, the controller may compute both desired catalyst activity, NOx, and NH3 profiles and catalyst sootblower, NH3 injection, and fuel and air injection operating parameters expected to attain those catalyst activity, NOx, and NH3 profiles. In another embodiment of the invention, a single indirect controller may result from the integration of the function of processor 512 and control interface 514. In this integrated embodiment, the indirect controller will compute and control the catalyst sootblower, NH3 injection, and fuel and air injection parameters necessary to attain the desired catalyst activity, NOx, and NH3 profiles specified by the output of controller 510.
Controllers 128, 310, 510 in the illustrated embodiments of the invention, are preferably implemented in software and run their respective models also, preferably software to perform the computations described herein, and are operable on a computer. The particular software used is not a critical feature of the invention and one of ordinary skill in the art will be able to write various programs to perform the functions described herein. The computer may include, e.g., data storage capacity, output devices, such as data ports, printers and monitors, and input devices, such as keyboards, and data ports. The computer may also include access to a database of historical information about the operation of the boiler. Processor 112 is a similar computer designed to perform the processor computations described herein.
As indicated above, various components of the SCR optimization system could be integrated. For example, the catalyst sootblower, NH3 injector, and fuel and air injector control interfaces 514, the processor 512, and the model-based controller 510 could be integrated into a single computer; alternatively model-based controller 310 and catalyst sootblower, NH3 injector, and fuel and air injector interfaces 314 could be integrated into a single computer. The controllers 128, 310 or 510 may include an override or switching mechanism so that efficiency set points or catalyst sootblower, NH3 injector, or fuel and air injector optimization parameters can be set directly, e.g., by an operator, rather than by the model-based controller when desired.
While the present invention has been illustrated and described with reference to preferred embodiments thereof, it will be apparent to those skilled in the art that modifications can be made and the invention can be practiced in other environments without departing from the spirit and scope of the invention.
This application is based on and claims priority from U.S. Provisional Patent Application Ser. No. 60/604,921 filed Aug. 27, 2004 and entitled Methods and Systems for SCR Optimization, the specification of which is incorporated by referenced herein in its entirety.
This invention was made with Government support under Contract Number DE-FC26-04NT41768 awarded by the U.S. Department of Energy. The Government has certain rights in the invention.
| Number | Date | Country | |
|---|---|---|---|
| 60604921 | Aug 2004 | US |
